CN114716306B - Method for hydroformylation of Fischer-Tropsch products - Google Patents
Method for hydroformylation of Fischer-Tropsch products Download PDFInfo
- Publication number
- CN114716306B CN114716306B CN202111461093.4A CN202111461093A CN114716306B CN 114716306 B CN114716306 B CN 114716306B CN 202111461093 A CN202111461093 A CN 202111461093A CN 114716306 B CN114716306 B CN 114716306B
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- Prior art keywords
- fischer
- pressure
- tropsch
- temperature
- synthesis gas
- Prior art date
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- 238000007037 hydroformylation reaction Methods 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 41
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 68
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 67
- 239000003054 catalyst Substances 0.000 claims abstract description 44
- 239000002904 solvent Substances 0.000 claims abstract description 10
- 238000003756 stirring Methods 0.000 claims description 100
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 63
- 239000007789 gas Substances 0.000 claims description 61
- 239000000203 mixture Substances 0.000 claims description 41
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 33
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 claims description 30
- 239000002253 acid Substances 0.000 claims description 28
- GGRQQHADVSXBQN-FGSKAQBVSA-N carbon monoxide;(z)-4-hydroxypent-3-en-2-one;rhodium Chemical group [Rh].[O+]#[C-].[O+]#[C-].C\C(O)=C\C(C)=O GGRQQHADVSXBQN-FGSKAQBVSA-N 0.000 claims description 26
- 238000002156 mixing Methods 0.000 claims description 24
- ZGEGCLOFRBLKSE-UHFFFAOYSA-N 1-Heptene Chemical compound CCCCCC=C ZGEGCLOFRBLKSE-UHFFFAOYSA-N 0.000 claims description 22
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 claims description 22
- JRZJOMJEPLMPRA-UHFFFAOYSA-N 1-nonene Chemical compound CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 18
- 229910052703 rhodium Inorganic materials 0.000 claims description 17
- 239000010948 rhodium Substances 0.000 claims description 17
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical group [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 17
- 239000003446 ligand Substances 0.000 claims description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 12
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 12
- 239000003513 alkali Substances 0.000 claims description 11
- 230000000536 complexating effect Effects 0.000 claims description 11
- 230000003213 activating effect Effects 0.000 claims description 10
- 150000001875 compounds Chemical class 0.000 claims description 9
- AFFLGGQVNFXPEV-UHFFFAOYSA-N 1-decene Chemical compound CCCCCCCCC=C AFFLGGQVNFXPEV-UHFFFAOYSA-N 0.000 claims description 8
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 claims description 8
- DCTOHCCUXLBQMS-UHFFFAOYSA-N 1-undecene Chemical compound CCCCCCCCCC=C DCTOHCCUXLBQMS-UHFFFAOYSA-N 0.000 claims description 8
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 7
- 239000002243 precursor Substances 0.000 claims description 7
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 claims description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 5
- TVMXDCGIABBOFY-UHFFFAOYSA-N n-Octanol Natural products CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 5
- ROSDSFDQCJNGOL-UHFFFAOYSA-N Dimethylamine Chemical compound CNC ROSDSFDQCJNGOL-UHFFFAOYSA-N 0.000 claims description 4
- QUSNBJAOOMFDIB-UHFFFAOYSA-N Ethylamine Chemical compound CCN QUSNBJAOOMFDIB-UHFFFAOYSA-N 0.000 claims description 4
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 claims description 4
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 4
- UXRZLDREKITWRO-UHFFFAOYSA-N P(c1ccccc1)c1ccccc1.CC1(C)c2ccccc2Oc2ccccc12 Chemical compound P(c1ccccc1)c1ccccc1.CC1(C)c2ccccc2Oc2ccccc12 UXRZLDREKITWRO-UHFFFAOYSA-N 0.000 claims description 4
- GETQZCLCWQTVFV-UHFFFAOYSA-N trimethylamine Chemical compound CN(C)C GETQZCLCWQTVFV-UHFFFAOYSA-N 0.000 claims description 4
- 239000008096 xylene Substances 0.000 claims description 4
- 239000012670 alkaline solution Substances 0.000 claims description 3
- HPNMFZURTQLUMO-UHFFFAOYSA-N diethylamine Chemical compound CCNCC HPNMFZURTQLUMO-UHFFFAOYSA-N 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 2
- 239000004711 α-olefin Substances 0.000 abstract description 19
- 239000002994 raw material Substances 0.000 abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 11
- 239000003245 coal Substances 0.000 abstract description 4
- 238000006243 chemical reaction Methods 0.000 description 59
- 238000004458 analytical method Methods 0.000 description 48
- 239000000047 product Substances 0.000 description 47
- 150000001336 alkenes Chemical class 0.000 description 28
- 238000004817 gas chromatography Methods 0.000 description 26
- 239000005457 ice water Substances 0.000 description 25
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 description 23
- CXNIUSPIQKWYAI-UHFFFAOYSA-N xantphos Chemical compound C=12OC3=C(P(C=4C=CC=CC=4)C=4C=CC=CC=4)C=CC=C3C(C)(C)C2=CC=CC=1P(C=1C=CC=CC=1)C1=CC=CC=C1 CXNIUSPIQKWYAI-UHFFFAOYSA-N 0.000 description 20
- 230000004913 activation Effects 0.000 description 15
- RIOQSEWOXXDEQQ-UHFFFAOYSA-N triphenylphosphine Chemical compound C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 RIOQSEWOXXDEQQ-UHFFFAOYSA-N 0.000 description 12
- 238000010668 complexation reaction Methods 0.000 description 11
- 239000003921 oil Substances 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 9
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000005070 sampling Methods 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- 150000001298 alcohols Chemical class 0.000 description 3
- 239000002199 base oil Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 238000006384 oligomerization reaction Methods 0.000 description 3
- VYFPSYVVFFFYBF-UHFFFAOYSA-N sodium;triphenylphosphane Chemical compound [Na].C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 VYFPSYVVFFFYBF-UHFFFAOYSA-N 0.000 description 3
- RYPKRALMXUUNKS-UHFFFAOYSA-N 2-Hexene Natural products CCCC=CC RYPKRALMXUUNKS-UHFFFAOYSA-N 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 150000001868 cobalt Chemical class 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- LPIQUOYDBNQMRZ-UHFFFAOYSA-N cyclopentene Chemical compound C1CC=CC1 LPIQUOYDBNQMRZ-UHFFFAOYSA-N 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- BKIMMITUMNQMOS-UHFFFAOYSA-N nonane Chemical compound CCCCCCCCC BKIMMITUMNQMOS-UHFFFAOYSA-N 0.000 description 2
- QMMOXUPEWRXHJS-UHFFFAOYSA-N pentene-2 Natural products CCC=CC QMMOXUPEWRXHJS-UHFFFAOYSA-N 0.000 description 2
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- RSJKGSCJYJTIGS-UHFFFAOYSA-N undecane Chemical compound CCCCCCCCCCC RSJKGSCJYJTIGS-UHFFFAOYSA-N 0.000 description 2
- GGQQNYXPYWCUHG-RMTFUQJTSA-N (3e,6e)-deca-3,6-diene Chemical compound CCC\C=C\C\C=C\CC GGQQNYXPYWCUHG-RMTFUQJTSA-N 0.000 description 1
- YCTDZYMMFQCTEO-FNORWQNLSA-N (E)-3-octene Chemical compound CCCC\C=C\CC YCTDZYMMFQCTEO-FNORWQNLSA-N 0.000 description 1
- GVRWIAHBVAYKIZ-FNORWQNLSA-N (e)-dec-3-ene Chemical compound CCCCCC\C=C\CC GVRWIAHBVAYKIZ-FNORWQNLSA-N 0.000 description 1
- JOHIXGUTSXXADV-HWKANZROSA-N (e)-undec-2-ene Chemical compound CCCCCCCC\C=C\C JOHIXGUTSXXADV-HWKANZROSA-N 0.000 description 1
- IICQZTQZQSBHBY-HYXAFXHYSA-N (z)-non-2-ene Chemical compound CCCCCC\C=C/C IICQZTQZQSBHBY-HYXAFXHYSA-N 0.000 description 1
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- LVLXQRZPKUFJJQ-UHFFFAOYSA-N 2,3-dimethylhex-1-ene Chemical compound CCCC(C)C(C)=C LVLXQRZPKUFJJQ-UHFFFAOYSA-N 0.000 description 1
- OTTZHAVKAVGASB-HYXAFXHYSA-N 2-Heptene Chemical compound CCCC\C=C/C OTTZHAVKAVGASB-HYXAFXHYSA-N 0.000 description 1
- OTTZHAVKAVGASB-UHFFFAOYSA-N 2-heptene Natural products CCCCC=CC OTTZHAVKAVGASB-UHFFFAOYSA-N 0.000 description 1
- SDTYFWAQLSIEBH-FNORWQNLSA-N 3-Undecene Chemical compound CCCCCCC\C=C\CC SDTYFWAQLSIEBH-FNORWQNLSA-N 0.000 description 1
- SDTYFWAQLSIEBH-UHFFFAOYSA-N 3-Undecene Natural products CCCCCCCC=CCC SDTYFWAQLSIEBH-UHFFFAOYSA-N 0.000 description 1
- 208000010444 Acidosis Diseases 0.000 description 1
- XYGKGASSKJWLTN-UHFFFAOYSA-N CCCCCCC.CCCCCCC Chemical compound CCCCCCC.CCCCCCC XYGKGASSKJWLTN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000007950 acidosis Effects 0.000 description 1
- 208000026545 acidosis disease Diseases 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 150000001721 carbon Chemical group 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- YKNMBTZOEVIJCM-UHFFFAOYSA-N dec-2-ene Chemical compound CCCCCCCC=CC YKNMBTZOEVIJCM-UHFFFAOYSA-N 0.000 description 1
- UURSXESKOOOTOV-UHFFFAOYSA-N dec-5-ene Chemical compound CCCCC=CCCCC UURSXESKOOOTOV-UHFFFAOYSA-N 0.000 description 1
- DIOQZVSQGTUSAI-NJFSPNSNSA-N decane Chemical compound CCCCCCCCC[14CH3] DIOQZVSQGTUSAI-NJFSPNSNSA-N 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- GPAYUJZHTULNBE-UHFFFAOYSA-N diphenylphosphine Chemical compound C=1C=CC=CC=1PC1=CC=CC=C1 GPAYUJZHTULNBE-UHFFFAOYSA-N 0.000 description 1
- VURFVHCLMJOLKN-UHFFFAOYSA-N diphosphane Chemical compound PP VURFVHCLMJOLKN-UHFFFAOYSA-N 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- WZHKDGJSXCTSCK-UHFFFAOYSA-N hept-3-ene Chemical compound CCCC=CCC WZHKDGJSXCTSCK-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- DIOQZVSQGTUSAI-UHFFFAOYSA-N n-butylhexane Natural products CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- KPADFPAILITQBG-UHFFFAOYSA-N non-4-ene Chemical compound CCCCC=CCCC KPADFPAILITQBG-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- GJVFBWCTGUSGDD-UHFFFAOYSA-L pentamethonium bromide Chemical compound [Br-].[Br-].C[N+](C)(C)CCCCC[N+](C)(C)C GJVFBWCTGUSGDD-UHFFFAOYSA-L 0.000 description 1
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 1
- 150000003003 phosphines Chemical class 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 150000003284 rhodium compounds Chemical group 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- TUQOTMZNTHZOKS-UHFFFAOYSA-N tributylphosphine Chemical compound CCCCP(CCCC)CCCC TUQOTMZNTHZOKS-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
- B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
- B01J31/2404—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G19/00—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment
- C10G19/02—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment with aqueous alkaline solutions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
- B01J2231/30—Addition reactions at carbon centres, i.e. to either C-C or C-X multiple bonds
- B01J2231/32—Addition reactions to C=C or C-C triple bonds
- B01J2231/321—Hydroformylation, metalformylation, carbonylation or hydroaminomethylation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
- B01J2531/80—Complexes comprising metals of Group VIII as the central metal
- B01J2531/82—Metals of the platinum group
- B01J2531/822—Rhodium
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Materials Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the field of Fischer-Tropsch synthesis and discloses a method for hydroformylation of a Fischer-Tropsch product. The method comprises the following steps: in the presence of a catalyst and a solvent, contacting a Fischer-Tropsch product with synthesis gas to carry out hydroformylation reaction; wherein the Fischer-Tropsch product comprises C 5 ‑C 11 Is a alpha-olefin of (c). The raw material adopted by the method is a coal-based Fischer-Tropsch synthesis product, and the Fischer-Tropsch synthesis product contains C 5 ‑C 11 Alpha-olefins of (C) such that C 5 ‑C 11 When the alpha-olefin is used as the raw material of the hydroformylation, the odd carbon chain alpha-olefin can be provided, and the variety of products is widened.
Description
Technical Field
The invention relates to the field of Fischer-Tropsch synthesis, in particular to a method for hydroformylation of a Fischer-Tropsch product.
Background
The hydroformylation reaction is also called OXO reaction, and refers to a reaction in which carbon monoxide and hydrogen can be added to an olefin in one step by a transition metal complex catalyst, and an aldehyde having one more carbon atom than the original olefin can be produced with an atom utilization efficiency of 100%. Generally, the linear and branched aldehydes produced by the hydroformylation reaction can be further converted to alcohols by hydrogenation reduction. This is the classical method of industrially producing plasticizer alcohols and surfactant alcohols.
The industry has catalyzed olefin hydroformylation using cobalt-based catalysts, with BASF corporation employing unmodified cobalt carbonyl HCo (CO) 4 As a catalyst, in the actual industrial application process, the unmodified cobalt catalyst usually needs higher reaction temperature (140-180 ℃) and reaction pressure (20-35 MPa) during the hydroformylation reaction, the reaction condition is harsh, and the selectivity of aldehyde in the reaction product is lower (HeckRF, breslowDS.Thereactionofcobalthydrotetracarbonylwitholefins [ J ]]Journ aloftheAmericanChemicalSociety,1961,83 (19): 4023-4027. Further, shell modified cobalt catalysts with trialkyl phosphines, such as tri-n-butyl-phosphorus, to form HCo (CO) 3 (PR 3 ) A catalyst of the type which requires a reduced pressure (5-10 MPa) compared to the BASF process for the hydroformylation of olefins, but which still requires a higher temperature (170-210 ℃) and the selectivity of the aldehydes in the product is still not satisfactory (US 3239569; US 3448157). Compared with the harsh reaction conditions of cobalt catalysts, rhodium catalysts have been attracting attention because of the mildness of the reaction conditions and good selectivity of the reaction products, DAVY company, UCC company, BASF company all use triphenylphosphine as phosphine ligand to modify rhodium catalysts to expect formation of HRh (CO) during the reaction x (PPh 3 ) 4-x The catalyst has a catalytic active center, and the reaction pressure is smaller (usually 1-15 MPa) and the reaction temperature is lower (100-130 ℃) when the catalyst is practically applied in industry (Rhodium catalyzedHydroxymyction [ M)].SpringerScience&BusinessMedia,2002.)。
Linear alpha-olefins as important raw materials for hydroformylation reactions can be produced initially by thermal cracking of paraffins, which can produce large quantitiesAn amount of alpha-olefins, a small amount of alkanes and internal olefins. Wherein, the mixture of internal olefin and alpha-olefin can be subjected to hydroformylation reaction through Co catalyst to further synthesize detergent alcohol; alpha-olefins may also be produced by dehydration of alpha-alkanols. However, these two methods are gradually abandoned by people because the reaction conditions are too severe. Then, people start to adopt a method of steam cracking long-chain alkane and catalytic cracking long-chain alkane to generate alkene and alkyne. C since the 70 th century of 20 th century 4 -C 18 The olefin of (2) is mainly produced by an ethylene oligomerization method provided by a Shell High Olefin Process (SHOP), but the method can only provide alpha-olefin with even carbon chain length to the market by ethylene oligomerization, and it is difficult to provide alpha-olefin with odd carbon chain type except propylene.
Moreover, in the prior art of coal-based Fischer-Tropsch olefin hydroformylation, the carbon chain length of the Fischer-Tropsch olefin used for the hydroformylation reaction is still short, the carbon chain length is limited to propylene and butene, and the normal-to-iso ratio of the product aldehyde is still low.
Disclosure of Invention
The invention aims to solve the problems that the raw materials of the hydroformylation reaction are limited, the normal-to-iso ratio of product aldehyde is still low, and an ethylene oligomerization method cannot obtain odd carbon chain alpha-olefin in the prior art, and provides a Fischer-Tropsch product hydroformylation method.
To achieve the above object, in one aspect, the present invention provides a method for hydroformylation of a fischer-tropsch product, the method comprising:
in the presence of a catalyst and a solvent, contacting a Fischer-Tropsch product with synthesis gas to carry out hydroformylation reaction; wherein the Fischer-Tropsch product comprises C 5 -C 11 Is a alpha-olefin of (c).
The invention provides a method for hydroformylation of Fischer-Tropsch products, which adopts coal-based Fischer-Tropsch synthesis products as raw materials, wherein the Fischer-Tropsch synthesis products contain C 5 -C 11 Alpha-olefins of (C) such that C 5 -C 11 When the alpha-olefin is used as the raw material of the hydroformylation, the odd carbon chain alpha-olefin can be provided, the normal and abnormal ratio of the product aldehyde is high, and the variety of the product is widened.
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
In one aspect, the invention provides a process for hydroformylation of a Fischer-Tropsch product. The method comprises the following steps:
in the presence of a catalyst and a solvent, contacting a Fischer-Tropsch product with synthesis gas to carry out hydroformylation reaction; wherein the Fischer-Tropsch product comprises C 5 -C 11 Is a alpha-olefin of (c).
In some embodiments of the invention, the weight ratio of the catalyst, the solvent and the fischer-tropsch product is 1 to allow the reaction to proceed efficiently: 8-80:95-1000, preferably 1:30-50:400-450.
In some embodiments of the invention, preferably, C in the Fischer-Tropsch product 5 -C 11 The content of alpha-olefins is 50 to 68 wt.%. Further preferably, the alpha-olefin comprises at least one of 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, and 1-undecene.
In some embodiments of the present invention, preferably, the Fischer-Tropsch product further comprises pentane, hexane, heptane, octane, nonane, decane, undecane, C 5 Isoolefins (e.g. 2-pentene and/or cyclopentene), C 6 Isoolefins (e.g. 2-hexene), C 7 Isoolefins (e.g. 2-heptene and/or 3-heptene), C 8 Isoolefins (e.g. 3-octene and/or 2, 3-dimethyl-1-hexene), C 9 Isoolefins (e.g. cis-2-nonene and/or 4-nonene), C 10 Isoolefins (e.g., at least one of 2-decene, trans-3-decene, and 5-decene), C 11 At least one of isoolefins (e.g., 2-undecene and/or 3-undecene) and oxygenates.
In the invention, the method can be as followsThe Fischer-Tropsch product is separated into fractions of different carbon chain lengths according to conventional methods, and each fraction is suitable for use in the process of the invention. According to a preferred embodiment of the invention, the Fischer-Tropsch product is Fischer-Tropsch C 5 Fractions of the Fischer-Tropsch C 5 The composition of the fractions is generally: 50-51wt% of 1-pentene, 40-41wt% of pentane and C 5 4-5wt% of isoolefin, 4-5wt% of oxygen-containing compound and 0.8-0.9mgKOH/g of acid value. According to another preferred embodiment of the invention, the Fischer-Tropsch product is C 6 Fractions of the Fischer-Tropsch C 6 The composition of the fractions is generally from 60 to 65% by weight of 1-hexene, from 25 to 30% by weight of hexane, C 6 6-8wt% of isoolefin, 4-5wt% of oxygen-containing compound and 1.7-1.8mgKOH/g of acid value. According to another preferred embodiment of the invention, the Fischer-Tropsch product is C 7 Fractions of the Fischer-Tropsch C 7 The composition of the fractions is generally from 60 to 65% by weight of 1-heptene, from 25 to 30% by weight of heptane, C 7 3-8wt% of isoolefin, 4-5wt% of oxygen-containing compound and 1.4-1.5mgKOH/g of acid value. According to another preferred embodiment of the invention, the Fischer-Tropsch product is C 5 -C 7 Fractions of the Fischer-Tropsch C 5 -C 7 The composition of the fractions is generally from 18 to 20% by weight of 1-pentene, from 20 to 23% by weight of 1-hexene, from 10 to 20% by weight of 1-heptene, C 5 -C 7 30-40wt% of mixed alkane and C 5 -C 7 4-5wt% of mixed isoolefin, 4-5wt% of oxygen-containing compound and 1.4-1.6mgKOH/g of acid value. According to another preferred embodiment of the invention, the Fischer-Tropsch product is C 5 -C 11 Fractions of the Fischer-Tropsch C 5 -C 11 The composition of the fraction is generally 1-pentene 2-5wt%, 1-hexene 10-15wt%, 1-heptene 15-20wt%, 1-octene 18-20wt%, 1-nonene 19-20wt%, 1-decene 0.1-1wt%, 1-undecene 0.1-1wt%, and C 5 -C 11 26.5 to 30 weight percent of mixed alkane and C 5 -C 11 1-2wt% of mixed isoolefin, 4-5wt% of oxygen-containing compound and 1.6-1.8mgKOH/g of acid value.
In the invention, the Fischer-Tropsch product obtaining method comprises the following steps: crude synthesis gas (H) obtained by indirect coal liquefaction 2 The +CO) is subjected to Fischer-Tropsch synthesis (F-T) reaction to generate Fischer-Tropsch products, and the catalyst can be an iron-based catalyst, a cobalt-based catalyst and a nickel-based catalyst, wherein the reaction conditions can beThe inventor of the present invention further found that the components of the Fischer-Tropsch product used in the present invention are complex and may contain acidic substances, which are toxic to rhodium-based catalytic systems and affect the stability of the catalyst, so that the existing catalyst cannot meet the requirements of hydroformylation reaction. To this end, the method further comprises: before the hydroformylation reaction, the Fischer-Tropsch product is mixed with alkali liquor for deacidification, so that the problem of acidosis of an oxo catalyst is effectively solved, the hydroformylation reaction is further promoted, the raw material conversion rate is improved, and the like. Preferably, the acid value of the mixture obtained after the deacidification treatment is not more than 0.05mgKOH/g.
In some embodiments of the present invention, to reduce the emulsification phenomenon and improve the deacidification effect, the weight ratio of the fischer-tropsch product to the alkaline solution is preferably 1:1-2.
In some embodiments of the invention, the Fischer-Tropsch product has an acid number of from 0.79 to 2.85mgKOH/g.
In some embodiments of the invention, preferably, the lye is present in a concentration of 0.5 to 5% by weight.
In some embodiments of the present invention, the alkaline substance in the alkaline solution is not particularly limited, and may be, for example, at least one selected from sodium hydroxide, potassium hydroxide, ammonia, methylamine, dimethylamine, trimethylamine, ethylamine, diethylamine, and triethylamine.
In some embodiments of the invention, the deacidification treatment is performed under stirring conditions to increase the conversion rate of the reaction and the selectivity of aldehyde, and the deacidification treatment conditions include: the temperature is 20-40 ℃, the pressure is 0.01-0.1MPa, the stirring speed is 400-800r/min, and the time is 200-300min.
In some embodiments of the invention, the catalyst is a rhodium compound, with which the positive to negative ratio of the product aldehyde can be up to 30 or more, in order to obtain higher selectivity to linear aldehyde.
In some embodiments of the invention, the catalyst is a rhodium-containing complex, preferably the weight ratio of rhodium precursor to ligand in the catalyst is 1:10-105, more preferably 1:10.2-102.
The rhodium catalyst of the invention can be recycled, the total TON can be up to 60978, the loss of rhodium metal in the recycling process is very little, and the production cost is saved.
In some embodiments of the invention, to prevent oxidation of the catalyst, it is preferred that the rhodium precursor is complexed with the ligand under anaerobic conditions prior to the hydroformylation reaction, and then activated in a reducing atmosphere. In the present invention, "oxygen-free" does not mean an absolute absence of oxygen, but means that the oxygen content is 100ppm by volume or less, but includes an absolute absence of oxygen. The oxygen in the reaction system can be replaced by filling inert gas into the reaction system so as to ensure that the complexation is carried out under the anaerobic condition. In the present invention, the optional range of the kind of the inert gas is wide, for example, one or more of nitrogen, argon and lower hydrocarbon. The reducing atmosphere can be H 2 And/or CO.
In the present invention, the activation is to increase the catalyst activity. In some embodiments of the invention, to enhance catalyst use, preferably, the complexing conditions include: the temperature is 20-40 ℃, the pressure is 0.01-0.1MPa, the stirring speed is 400-800r/min, and the time is 10-15h.
In some embodiments of the invention, to increase catalyst activity, preferably, the activating conditions include: the pressure is 1-7MPa, the temperature is 90-120 ℃, the stirring speed is 400-800r/min, and the time is 0.5-2h.
In some embodiments of the invention, preferably, the rhodium precursor is selected from Rh (acac) (CO) 2 And/or HRh (CO) 4 。
In some embodiments of the invention, preferably, the ligand of the catalyst is selected from a monophosphine ligand or a biphosphine ligand, preferably triphenylphosphine (formula (1), abbreviated PPh 3 ) And/or 4, 5-bis (diphenylphosphine) -9, 9-dimethylxanthene (structural formula (2), abbreviated as XantPhos). Wherein, the structural formula of triphenylphosphine is:
the structural formula of the 4, 5-bis (diphenylphosphine) -9, 9-dimethyl xanthene is as follows:
in some embodiments of the invention, the catalyst is selected from HRh (CO) 3 (PPh 3 )、HRh(CO) 2 (PPh 3 ) 2 、HRh(CO)(PPh 3 ) 3 And HRh (CO) 2 At least one of (XantPhos).
In some embodiments of the present invention, preferably, the solvent is selected from at least one of toluene, xylene, and benzene.
In some embodiments of the invention, preferably, H in the synthesis gas 2 And the molar ratio of CO is 1-2.
In some embodiments of the invention, the synthesis gas is used in an amount such that the hydroformylation reaction is at a pressure of 1 to 7MPa, preferably 3 to 4MPa, to enhance the reaction.
In some embodiments of the invention, the hydroformylation reaction is carried out under agitation.
In some embodiments of the invention, the hydroformylation reaction conditions include: the temperature is 90-120 ℃, the stirring speed is 400-800r/min, and the time is 1-6h.
In the present invention, after the hydroformylation reaction is completed, the resulting mixture is distilled (for example, may be distilled under reduced pressure) to obtain aldehyde, and the remaining residual liquid is recycled as a catalyst phase.
According to a specific embodiment of the invention, the hydroformylation reaction of the invention is carried out as follows:
(1) Contacting a rhodium precursor with a ligand to complex and activate;
(2) Mixing the Fischer-Tropsch product with alkali liquor for deacidification;
(3) In the presence of the catalyst and the solvent obtained in the step (1), the mixture obtained in the step (2) is contacted with synthesis gas to carry out hydroformylation reaction; specifically, the gas in the high-pressure reaction kettle is replaced by synthesis gas, and then the synthesis gas with a specified pressure (such as 1-7MPa, preferably 3-4 MPa) is filled for hydroformylation reaction.
The present invention will be described in detail by examples. In the following examples and comparative examples, the Fischer-Tropsch product compositions are shown in tables 1-5, and in addition, the various starting materials used were all commercially available, unless otherwise specified.
The composition of the various carbon chain length fractions of each Fischer-Tropsch product is shown in tables 1-5 below:
table 1 shows Fischer-Tropsch C 5 Fraction raw material composition
Table 2 shows Fischer-Tropsch C 6 Fraction raw material composition
Numbering device | Component (A) | Content/wt% |
1 | 1-hexene | 63.74 |
2 | Hexane | 25.74 |
3 | C 6 Isomerised olefins | 6.19 |
4 | Oxygen-containing compound | 4.33 |
5 | Acid value/mgKOH/g | 1.71 |
Table 3 shows Fischer-Tropsch C 7 Fraction raw material composition
Numbering device | Component (A) | Content/wt% |
1 | 1-heptene | 63.28 |
2 | Heptane (heptane) | 29.35 |
3 | C 7 Isomerised olefins | 3.09 |
4 | Oxygen-containing compound | 4.28 |
5 | Acid value/mgKOH/g | 1.48 |
Table 4 shows Fischer-Tropsch C 5 -C 7 Fraction raw material composition
Table 5 shows Fischer-Tropsch C 5 -C 11 Fraction raw material composition
Numbering device | Component (A) | Content/wt% |
1 | 1-pentene | 2.77 |
2 | 1-hexene | 10.41 |
3 | 1-heptene | 15.68 |
4 | 1-octene | 18.6 |
5 | 1-nonene | 19.67 |
6 | 1-decene | 0.12 |
7 | 1-undecene | 0.11 |
8 | C 5 -C 11 Mixed alkanes | 26.93 |
9 | C 5 -C 11 Mixed isoolefins | 1.35 |
10 | Oxygen-containing compound | 4.36 |
11 | Acid value/mgKOH/g | 1.69 |
Example 1
Will 1 mg Rh (acac) (CO) 2 10.2 mg PPh 3 Mixing with 0.866 g toluene, complexing (20 ℃ C., 0.01MPa, stirring speed 400r/min, time 10 h) and activating (1 MPa, 90 ℃ C., stirring speed 400r/min, time 0.5 h), then mixing the activated mixture with 10.165 g of undeacidification Fischer-Tropsch 1-pentene (Fischer-Tropsch C of Table 1) 5 Fraction) was charged into a high-pressure reaction vessel with a temperature controller and a magnetic stirrer, and P was introduced into the vessel H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and a stirring speed of 800rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 2
Will 1 mg Rh (acac) (CO) 2 60 mg PPh 3 After mixing with 0.898 g of toluene, complexation (temperature 40 ℃ C., pressure 0.01MPa, stirring rate 500r/min, time 15 h) and activation (pressure 7MPa, temperature 120 ℃ C., stirring rate 800r/min, time 2 h) were carried out, and the activated mixture was then reacted with 11.02 g of non-deacidified Fischer-Tropsch 1-hexene (Fischer-Tropsch C of Table 2) 6 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1: 2, replacing air for three times, then adding the synthesis gas into a kettle to enable the pressure of the system to be 3MPa, reacting for 4 hours at the temperature of 110 ℃ and the stirring speed of 500rpm, rapidly cooling in an ice water bath, decompressing, opening the kettle, sampling, and performing gas chromatography analysis, wherein the analysis result is shown in table 6.
Example 3
Will 1 mg Rh (acac) (CO) 2 102 mg PPh 3 Mixing with 0.91 g toluene, complexing (30 deg.C, 0.05MPa, stirring speed)At a rate of 800r/min for 13 h) and activation (pressure of 3MPa, temperature of 110 ℃, stirring rate of 600r/min for 1 h), the activated mixture was then reacted with 10.13 g of undedeacidified Fischer-Tropsch 1-heptene (Fischer-Tropsch C of Table 3) 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1: 1.2, replacing air for three times, then adding the synthesis gas into a kettle to enable the pressure of the system to be 7MPa, reacting for 6 hours at the temperature of 100 ℃ and the stirring speed of 400rpm, rapidly cooling in an ice water bath, decompressing, opening the kettle, sampling, and performing gas chromatography analysis, wherein the analysis result is shown in Table 6.
Example 4
Will 1 mg Rh (acac) (CO) 2 16.2 mg PPh 3 Mixing with 0.866 g toluene, complexing (30 deg.C, 0.05MPa, 800r/min stirring speed, 13 h) and activating (3 MPa, 110 deg.C, 600r/min stirring speed, 1 h), mixing with 10.165 g of undeacidification Fischer-Tropsch C 5 -C 7 Mixed olefins (Fischer-Tropsch C of Table 4) 5 -C 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 5
Will 1 mg Rh (acac) (CO) 2 18.2 mg PPh 3 Mixing with 0.866 g toluene, complexing (30 deg.C, 0.05MPa, 800r/min stirring speed, 13 h) and activating (3 MPa, 110 deg.C, 600r/min stirring speed, 1 h), mixing with 10.165 g of undeacidification Fischer-Tropsch C 5 -C 11 (Fischer-Tropsch C of Table 5) 5 -C 11 Fraction) of mixed olefins, with temperature controlIn a high-pressure reaction kettle with a magnetic stirrer, P is introduced into the kettle H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 6
Will 1 mg Rh (acac) (CO) 2 10.2 mg PPh 3 And 0.866 g of toluene (30 ℃ C., 0.05MPa, 800r/min stirring rate, 13 h) and activation (3 MPa, 110 ℃ C., 600r/min stirring rate, 1 h) were mixed, and the activated mixture was then mixed with 10.165 g of 5wt% aqueous ammonia solution in an alkali oil weight ratio of 1:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) Fischer-Tropsch 1-pentene (before deacidification, fischer-Tropsch C of Table 1) having an acid number of 0.04mgKOH/g 5 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 7
Will 1 mg Rh (acac) (CO) 2 10.2 mg PPh 3 And 0.866 g of toluene (30 ℃ C., 0.05MPa, 800r/min stirring rate, 13 h) and activation (3 MPa, 110 ℃ C., 600r/min stirring rate, 1 h) were mixed, and the activated mixture was then mixed with 10.165 g of an aqueous 3wt% ammonia solution in an alkali oil weight ratio of 2:1 (temperature 20 ℃ C., pressure 0.1MPa, stirring rate 500r/min, time 240 min) and acid value 0.05mgKOH/g of Fischer-Tropsch 1-pentene (before deacidification, fischer-Tropsch C of Table 1) 5 Fraction), with temperature controller and magnetIn a high-pressure reaction kettle with a force stirrer, P is introduced into the kettle H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 8
Will 1 mg Rh (acac) (CO) 2 10.2 mg PPh 3 After mixing with 0.866 g of toluene, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of a 5wt% diethylamine solution in a base oil weight ratio of 2:1 (temperature 40 ℃ C., pressure 0.05MPa, stirring rate 600r/min, time 250 min) and acid value 0.05mgKOH/g of Fischer-Tropsch 1-pentene (before deacidification, fischer-Tropsch C of Table 1) 5 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 9
Will 1 mg Rh (acac) (CO) 2 51 mg PPh 3 After mixing with 0.866 g of toluene, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of potassium hydroxide solution 3wt% in an alkali oil weight ratio 1:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 400r/min, time 240 min) and acid value 0.02mgKOH/g of Fischer-Tropsch 1-pentene (before deacidification, fischer-Tropsch C of Table 1) 5 Fraction), with temperature controller and magnetIn a high-pressure reaction kettle with a force stirrer, P is introduced into the kettle H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 10
Will 1 mg Rh (acac) (CO) 2 89 mg PPh 3 And 0.866 g of toluene (30 ℃ C., 0.05MPa, 800r/min stirring rate, 13 h) and activation (3 MPa, 110 ℃ C., 600r/min stirring rate, 1 h) were mixed, and the activated mixture was then mixed with 10.165 g of 1wt% potassium hydroxide solution in an alkali oil weight ratio of 2:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) and acid value 0.02mgKOH/g of Fischer-Tropsch 1-pentene (Fischer-Tropsch C of Table 1 before deacidification) 5 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 11
Will 1 mg Rh (acac) (CO) 2 94 mg PPh 3 After mixing with 0.866 g of toluene, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of sodium hydroxide solution 3wt% in a base oil weight ratio 1:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 250 min) Fischer-Tropsch 1-pentene (Fischer-Tropsch C of Table 1 before deacidification) having an acid value of 0.03mgKOH/g 5 Fraction), with a temperature controller andin a high-pressure reaction kettle of a magnetic stirrer, P is introduced into the kettle H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 12
Will 1 mg Rh (acac) (CO) 2 102 mg PPh 3 After mixing with 0.866 g of toluene, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of sodium hydroxide solution 2 wt.%: 1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) Fischer-Tropsch 1-pentene (before deacidification, fischer-Tropsch C of Table 1) having an acid number of 0.04mgKOH/g 5 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 13 (cycle test)
The reaction solution obtained in example 10 was distilled under reduced pressure under argon protection (column bottom temperature 80-115 ℃, column top temperature 35-73.5 ℃, vacuum degree 85kPa, column plate number 23, reflux ratio 3:2), after removing most of the product, a small amount of residual liquid at the bottom of the reactor containing the catalyst remained, transferred to a high-pressure reactor, and 10.165 g of sodium hydroxide solution 2wt% was added according to the weight ratio of alkali oil 2:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) and acid value 0.03mgKOH/g of Fischer-Tropsch 1-pentene (before deacidification, fischer-Tropsch C of Table 1) 5 Fraction), and then the mixture is introduced into a kettleP in H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, after 1 hour of reaction at 100 ℃ with stirring speed of 400rpm, rapid cooling was performed in an ice water bath, then pressure was released, the kettle was opened, and gas chromatography was performed by sampling. This operation was repeated 7 times, and the analysis results are shown in Table 7.
Example 14
Will 1 mg Rh (acac) (CO) 2 56 mg PPh 3 After mixing with 0.866 g of toluene, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of sodium hydroxide solution 2 wt.%: 1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) and acid value 0.04mgKOH/g of Fischer-Tropsch 1-hexene (before deacidification, fischer-Tropsch C of Table 2) 6 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 15
Will 1 mg Rh (acac) (CO) 2 34 mg PPh 3 After mixing with 0.866 g of toluene, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of sodium hydroxide solution 2 wt.%: 1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) and acid value 0.04mgKOH/g of Fischer-Tropsch 1-heptene (before deacidification, fischer-Tropsch C of Table 3) 7 Fraction), high pressure reaction with temperature controller and magnetic stirrerIn the reactor, P is introduced into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 16
Will 1 mg Rh (acac) (CO) 2 102 mg PPh 3 And 0.866 g of xylene, and then carrying out complexation (at a temperature of 30 ℃ C., a pressure of 0.05MPa, a stirring rate of 800r/min, a time of 13 h) and activation (at a pressure of 3MPa, a temperature of 110 ℃ C., a stirring rate of 600r/min, a time of 1 h), and then mixing the activated mixture with 10.165 g of a 3wt% potassium hydroxide solution in an alkali oil weight ratio of 1:1 acid value of 0.04mgKOH/g after deacidification (temperature: 30 ℃ C., pressure: 0.01MPa, stirring rate: 500r/min, time: 240 min) 5 -C 7 Mixed olefins (Fischer-Tropsch C of Table 4 before deacidification) 5 -C 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 17
Will 1 mg Rh (acac) (CO) 2 102 mg PPh 3 After mixing with 0.866 g benzene, complexing (temperature 30 ℃ C., pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activating (pressure 3MPa, temperature 110 ℃ C., stirring rate 600r/min, time 1 h), the activated mixture was then mixed with 10.165 g of 3wt% potassium hydroxide solution in a base oil weight ratio of 1:1 acid value of 0.03mgKOH/g after deacidification (temperature: 30 ℃ C., pressure: 0.01MPa, stirring rate: 500r/min, time: 240 min) 5 -C 11 (Fischer-Tropsch C of Table 5 before deacidification) 5 -C 11 Fraction) of mixed olefins, with addition of a catalyst having a temperatureDegree ofIn a high-pressure reaction kettle of a controller and a magnetic stirrer, P is introduced into the kettle H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 18
Will 1 mg Rh (acac) (CO) 2 After mixing 22.5 mg XantPhos and 0.866 g toluene, complexing (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activating (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h), the activated mixture was then reacted with 10.165 g of non-deacidified Fischer-Tropsch 1-hexene (Fischer-Tropsch C of Table 2) 6 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 19
Will 1 mg Rh (acac) (CO) 2 After mixing 22.5 mg XantPhos and 0.866 g toluene, complexing (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activating (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h), the activated mixture was then reacted with 10.165 g of non-deacidified Fischer-Tropsch 1-heptene (Fischer-Tropsch C of Table 3) 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, and after reacting at 100 ℃ with stirring speed of 400rpm for 1 hour,rapidly cooling in ice water bath, then decompressing, opening the kettle, sampling, and analyzing by gas chromatography, wherein the analysis result is shown in Table 6.
Example 20
Will 1 mg Rh (acac) (CO) 2 Mixing 22.5 mg XantPhos and 0.866 g toluene, complexing (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activating (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h), then mixing the activated mixture with 10.165 g of undeacidification Fischer-Tropsch C 5 -C 7 Mixed olefins (Fischer-Tropsch C of Table 4) 5 -C 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 2 hours at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 21
Will 1 mg Rh (acac) (CO) 2 Mixing 22.5 mg XantPhos and 0.866 g toluene, complexing (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activating (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h), then mixing the activated mixture with 10.165 g of undeacidification Fischer-Tropsch C 5 -C 11 Mixed olefins (Fischer-Tropsch C of Table 5) 5 -C 11 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 2 hours at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 22
Will 1 mg Rh (acac) (CO) 2 22.5 mg XantPhos and 0.866 gToluene was mixed and then subjected to complexation (temperature: 30 ℃, pressure: 0.05MPa, stirring rate: 800r/min, time: 13 h) and activation (pressure: 3MPa, temperature: 110 ℃, stirring rate: 600r/min, time: 1 h), and then the activated mixture was mixed with 10.165 g of a 2wt% sodium hydroxide solution in an alkali oil weight ratio of 2:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) and acid value 0.04mgKOH/g of Fischer-Tropsch 1-hexene (before deacidification, fischer-Tropsch C of Table 2) 6 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:2 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 4MPa, the reaction was carried out for 1 hour at 120 ℃ and stirring speed of 800rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 23
Will 1 mg Rh (acac) (CO) 2 22.5 mg XantPhos and 0.866 g toluene were mixed and then complexed (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activated (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h), the activated mixture then being admixed with 10.165 g of a 2% strength by weight sodium hydroxide solution in an alkaline oil weight ratio of 2:1 (temperature 30 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) and acid value 0.04mgKOH/g of Fischer-Tropsch 1-heptene (before deacidification, fischer-Tropsch C of Table 3) 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1.5, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 3 hours at 110 ℃ with stirring speed of 600rpm, then rapid cooling was carried out in an ice-water bath, then the kettle was opened by pressure relief, and the analysis was carried out by sampling and gas chromatography, and the analysis results were shown in table 6.
Example 24
Will 1 mg Rh (acac) (CO) 2 22.5 mg XantPhos and 0.866 g benzene were mixedAfter the combination, complexation (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activation (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h) were carried out, and then the activated mixture was mixed with 10.165 g of 3wt% potassium hydroxide solution according to an alkali oil weight ratio 1:1 acid value of 0.04mgKOH/g after deacidification (temperature 20 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) 5 -C 7 Mixed olefins (Fischer-Tropsch C of Table 4 before deacidification) 5 -C 7 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 3MPa, the reaction was carried out for 2 hours at 90 ℃ and a stirring speed of 500rpm, then the temperature was rapidly reduced in an ice-water bath, the kettle was opened by pressure relief, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 25
Will 1 mg Rh (acac) (CO) 2 22.5 mg XantPhos and 0.866 g xylene are mixed and then complexed (temperature 30 ℃, pressure 0.05MPa, stirring rate 800r/min, time 13 h) and activated (pressure 3MPa, temperature 110 ℃, stirring rate 600r/min, time 1 h), the activated mixture is then mixed with 10.165 g of 3% by weight potassium hydroxide solution in an alkaline oil weight ratio 1:1 acid value of 0.03mgKOH/g after deacidification (temperature 40 ℃, pressure 0.01MPa, stirring rate 500r/min, time 240 min) 5 -C 11 Mixed olefins (Fischer-Tropsch C of Table 5 before deacidification) 5 -C 11 Fraction), and then charging into a high-pressure reactor equipped with a temperature controller and a magnetic stirrer, and charging P into the reactor H2 :P CO (molar ratio) =1:1 synthesis gas, air was replaced three times, then synthesis gas was added to the kettle so that the pressure of the system was 1MPa, the reaction was carried out for 1 hour at 100 ℃ and stirring speed of 400rpm, then the temperature was rapidly lowered in an ice-water bath, the pressure was released, the kettle was opened, and the sample was taken for gas chromatography analysis, and the analysis results were shown in table 6.
Example 26
The Fischer-Tropsch product was hydroformylated as in example 1, except that PPh was hydroformylated 3 Replaced by triphenylphosphine sodium tri-m-sulfonate.
Test case
The product aldehydes obtained in the examples and comparative examples were analyzed by gas chromatograph, model GC-2014. Gas chromatography detection conditions: the sample injection amount is 0.2 mu L, the split ratio is 100, the sample injection port temperature is 250 ℃, the detector temperature is 250 ℃, the chromatographic column temperature is 35 ℃ (15 min) -2 ℃/min-200 ℃ (0 min) in a temperature program, and the carrier gas is nitrogen (95 kPa). Chromatographic column: HP-PONA (50 m.times.0.2 mm.times.0.5 μm). Wherein alpha-olefin means C 5 -C 11 The aldehydes in the selectivity of the product aldehydes include C 6 -C 12 Normal aldehyde and isomeric aldehyde of (2), the normal-to-iso ratio of product aldehyde refers to C in the product 6 -C 12 Normal aldehyde and C 6 -C 12 Is used as the catalyst.
The conversion rate and the like are calculated as follows:
the results obtained are shown in Table 6, and the test results of example 13 are shown in Table 7.
TABLE 6
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TABLE 7
As can be seen from the results in Table 6, in examples 1-26, the deacidified Fischer-Tropsch olefins had higher feed conversion and higher product aldehyde selectivity than the non-deacidified Fischer-Tropsch olefins, indicating that the deacidified Fischer-Tropsch olefins were better in catalyst activity. As can be seen from the results of examples 6 to 17, the hydroformylation reaction was carried out with triphenylphosphine as ligand and for Fischer-Tropsch C 5 -C 7 Deacidifying the olefin to obtain C 5 -C 7 The conversion of olefins was not less than 89wt%, the selectivity of product aldehyde was not less than 93.7wt%, the normal-to-iso ratio of product aldehyde was not more than 3.3, fischer-Tropsch C of example 17 5 -C 11 The conversion rate of the mixed olefin is only 72.7%, which shows that the ligand triphenylphosphine is suitable for the hydroformylation of Fischer-Tropsch olefins with shorter carbon chains and low requirement on the normal-to-iso ratio of aldehyde. As can be seen from the results of examples 22-25, the preferred ligand 4, 5-bis (diphenylphosphine) -9, 9-dimethylxanthene is suitable for hydroformylation of Fischer-Tropsch olefins with longer carbon chains, the conversion rate is greater than or equal to 94.8%, the selectivity is greater than or equal to 94.4%, the normal-to-iso ratio is greater than or equal to 28.2, the phosphine ligand of example 26 is triphenylphosphine sodium trimetaphosphate, the conversion rate, the selectivity and the normal-to-iso ratio of the obtained product are poor, and the effect of using triphenylphosphine and 4, 5-bis (diphenylphosphine) -9, 9-dimethylxanthene ligand is better than that of triphenylphosphine sodium trimetaphosphate. The cyclic test of example 13 shows that after 7 reactions, the conversion rate of the raw materials is reduced, because the catalyst is easy to deactivate at high temperature and is easy to oxidize, and the catalyst is deactivated during reduced pressure distillation, but the selectivity and the positive-to-negative ratio of the product aldehyde are not changed greatly, which means that rhodium loss is very little, and the production cost is saved.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (13)
1. A process for the hydroformylation of a fischer-tropsch product, the process comprising:
in the presence of a catalyst and a solvent, contacting a Fischer-Tropsch product with synthesis gas to carry out hydroformylation reaction;
the method further comprises the steps of: before the hydroformylation reaction, mixing a Fischer-Tropsch product with alkali liquor for deacidification;
the deacidification treatment is carried out under the condition of stirring, and the conditions of the deacidification treatment comprise: the temperature is 20-40 ℃, the pressure is 0.01-0.1MPa, the stirring speed is 400-800r/min, and the time is 200-300min;
the catalyst is a rhodium-containing complex; wherein the weight ratio of rhodium precursor to ligand used for preparing the rhodium-containing complex is 1:10-105; the ligand is selected from 4, 5-bis (diphenylphosphine) -9, 9-dimethylxanthene; the rhodium precursor is selected from Rh (acac) (CO) 2 ;
The consumption of the synthesis gas is such that the pressure of the hydroformylation reaction is 1-7MPa;
the hydroformylation reaction is carried out under stirring;
the conditions of the hydroformylation reaction include: the temperature is 90-120 ℃, the stirring speed is 400-800r/min, and the time is 1-6h;
the Fischer-Tropsch product is C 5 -C 11 Fractions of the Fischer-Tropsch C 5 -C 11 The composition of the fractions was: 2-5wt% of 1-pentene, 10-15wt% of 1-hexene, 15-20wt% of 1-heptene, 18-20wt% of 1-octene, 19-20wt% of 1-nonene, 0.1-1wt% of 1-decene, 0.1-1wt% of 1-undecene and C 5 -C 11 26.5 to 30 weight percent of mixed alkane and C 5 -C 11 1-2wt% of mixed isoolefin, 4-5wt% of oxygen-containing compound and 1.6-1.8mgKOH/g of acid value.
2. The process of claim 1, wherein the weight ratio of the catalyst, the solvent and the fischer-tropsch product is 1:8-80:95-1000.
3. The process of claim 1, wherein the weight ratio of the catalyst, the solvent and the fischer-tropsch product is 1:30-50:400-450.
4. The process according to claim 1 or 2, wherein the weight ratio of fischer-tropsch product to lye is 1:1-2.
5. The process according to claim 4, wherein the lye is present in a concentration of 0.5 to 5% by weight.
6. The method according to claim 4, wherein the alkaline substance in the alkaline solution is at least one selected from the group consisting of sodium hydroxide, potassium hydroxide, ammonia, methylamine, dimethylamine, trimethylamine, ethylamine, diethylamine and triethylamine.
7. The method according to claim 1, wherein the acid value of the mixture obtained after the deacidification treatment is 0.05mgKOH/g or less.
8. The process according to claim 1 or 7, wherein the rhodium precursor is complexed with the ligand under anaerobic conditions prior to the hydroformylation reaction and then activated in a reducing atmosphere.
9. The method of claim 8, wherein the complexing conditions comprise: the temperature is 20-40 ℃, the pressure is 0.01-0.1MPa, the stirring speed is 400-800r/min, and the time is 10-15h.
10. The method of claim 8, wherein the activating conditions comprise: the pressure is 1-7MPa, the temperature is 90-120 ℃, the stirring speed is 400-800r/min, and the time is 0.5-2h.
11. The method of any one of claims 1, 2 and 7, wherein the solvent is selected from at least one of toluene, xylene and benzene.
12. The method of any one of claims 1, 2, and 7, wherein H in the synthesis gas 2 And the molar ratio of CO is 1-2.
13. The process of claim 1 wherein the synthesis gas is used in an amount such that the hydroformylation reaction is at a pressure of from 3 to 4MPa.
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